Process tor generating isopropyl alcohol from hydrocarbons containing



Feb 9, 1932- H. s. DAvls ET AL PROCESS FOR GENERATING ISOPROPYL ALCOHOL FROM HYDROCARBONS CONTAINING QLEFINES original Filed Feb. `4, 1925 WiL/.ntf .f MMP/My Patentes' Feb. 9, 1932 UNITEDv STATES PATENT OFFICE;

HAROLD S. DAVIS, OF BELMONT, AND WALLACE J. MURRAY, OF READING, MASSACHU-l ETTS, ASSIGNORS, BY MESNE ASSIGNMENTS, TO PETROLEUM CHEMICAL CORPORA- TION, 0F NEW YORK, N. Y., A CORPORATION OF DELAWARE PROCESS FOR GENBATING ISOPIROPYL ALCOHOL FROM HYDROCARBONS CONTAINING OLEFINES l Original application led February 24, 1925, Serial No. 10,992, and in Germany February 23, 1926. Divided and this application led March 28, 1930. Serial No. 439,655.

This application is a division of parent application, Serial No. 10,992, filed February 24, 1925.

This invention relates to the preparation, segregation and utilization of oleiine hydrocarbons and to the production of their derivatives, including alcohols and other useful substances.l The oleines may be' derived from such materials as petroleum, peat, coal, oil shales, and like carboniferous natural materials by cracking or pyrogenesis,V so called.

The olene mixtures produced by heating such substances to temperatures resulting in pyrogenetic transformations are, as is well known, exceedingly complex, generally containing ethylene, propylene, butylenes, amylenes, hexylenes and higher oleiines of the general formula CDH. Unlike saturated hydrocarbons, oleiines are capable of readily reacting or combining with reagents, including the polybasic acids gef which sulphuric acid/- or phosphoric aci are typical) the halogens and halogen compounds, hypochlorous and other acids.

The reactionof sulphuric acid with the olefines has been known sincemits discovery in Faradays laboratory in 1826, and alcohols have been prepared from alkyl sulphu'ric acid products ofthis reaction on certain olefines by hydrolysis and distillation by numerous investigators sinceV Berthelots research in 1863.`A

Derivatives of olefines have beenmade on a commercial scale in this country by firstpreparing an acid reactive liquor of sulphurlc acid with oil gas since as early as 1906 (American Ether Company of Richmond, Virginia; P. Fritzsche, Zeitschrift fur angewandte Chemie, 1896, pp. 456, 459 Die Chemische lndustrie, vol.- 35, p. 637, 1912). Gases produced in the liquid phase cracking of petroleum` have Abeen similarly treated for the recovery of alcoholic mixtures including iso-V propyl, secondary butyl and amyl alcohols. These treatments, so far as we are aware, have -been of a kind adapted to the incidental recovery at gas works or petroleum pressure stills of gases from cracking operations rarely containing more than 12% of oletines, and free from any substantial contents of very reactive highly cracked hydrocarbons such as the dioleines. When any attempt has been made to produce industrially from mixed oleine bearing gases, such as the Waste gases from liquid phase cracking, acid reactive liquors capable of hydrolysis and distillation to obtain alcohols, sulphation has been carried out, so far as we are aware, b

reaction upon the Whole gaseous mixture'witli acid of a degree of concentration selected to reach a result necessarily inthe nature of a compromise between .destruction .by polymerization o r otherwise of the more reactive oleiines, and incomplete sulphation; and hence, with partial recovery only of the realizable oleine values and with high acid consumption. Such processes are economicall justifiable only When lean gases are av'ailab e in great quantities otherwise Wasted. Theyare not so justifiable when the gas to be treated is rich in olefines soreactive as to 'be converted into polymers while making the oleline-acid compound oa less reactive remainder. When the oleine bearing gas is rich in highly reactive o lenes, a singlefstage treatment to obtain acid products cannot be practised; the reaction of the morelhighly reactive olefines and other hydrocarbons to polymer under treatment with acids capable of forming addition compounds with the less reactive oleiines is too vigorous and too productive of heat to permit this even in theY case of relatively lean gases.

The known procedure has therefore been to destroy the very reactable olefines in one lot of acid, and sulphate the remainder in another vlot of acid.l

If it were ypracticable to obtain mixed alkyl I acid compounds and other derivatives of the' rich gases, such as result -from vapor hase cracking directed to the production o olehave boiling points ranging from A80" to 140 C., and separation from each other is in most cases not feasible. The uses of these alcohols (e. g. isopropyl and am l alcohols) The different kare widely divergent, and to pro uce them in admixture would be commercially kundesirable.

' hydrocarbons such as the diole This process provides a treatment of olene hydrocarbons, liquid or gaseous, particularly mixed hydrocarbons resulting from as complete eneration of these substances as possible rom a suitable hydrocarbon material or carboniferous material'l of the classes above enumerated, and therefore occurring richly in the material presented for treatment, and containing the very reactive hifgrhly cracked es, isobutlen'e, trimethylethylene, unsymmetrical met yl-ethyl-ethylene, and other unsaturated bodies having a high reactive ainity for combining acids or other reactants, and also containing other olenes of a lower order of reactivity toward the said combining agents; for example propylene, isopropyl, ethylene, butene-l, butene-Q, pentene-l and pentene-Q.

This new process thus provides a mode of treatment ap licable to hydrocarbon products rich in ighly reactive or unsaturated oleiinestorecover valuable derivatives and segregate the o leiine substances in the order of their chemical activities toward reagent' i ,into fractions substantially according to the order of the molecular weights of their principal contents, and the treatment severally of these fractions for the optimum production of valuable derivatives, e.- g., the l'appropriate alcohols, in a relatively pure and unmixed state; and without substantial destruction at any stage of this separation of any of the several fractions at the respective stage of the operations. A, n

The process`v conserves for use at a further stage of the process such of the reactive olecomprises a stagev or stages of separation of a fraction or fractions of the material contammg the olefne o'r olene groups to be recovered, followed by treatment selectively to differentiate and segregate the component oleines substances in accordance with their respective and relative chemical reactivities. In general it may be stated that the preferred raw material contains more than 30% of unsaturated hydrocarbons.

It is advantageous, inthe practice of this process, to proceed upon a basis of known contents of the raw material, and for this purpose'ial preferred vrraw material for the process is petroleum, treated by any process of vapor phase cracking tending-to produce a product rich in olefines and preferably ing a'substantial time of flow, this constant temperature being such as to result in optimum development of olefine values. For this v purpose, a cracking temperature maintained nearly constant at a selected value between 600 C. and 650 C. during a sufficient time l of flow to produce from 1000 .to 1700 cubic feet of gaseous product per barrel of 42 gallons passed produces satisfactory material for this treatment. The preferred vaporphase cracking temperatures are higher than those heretofore known for. the commercial production of motor spirit, which do not exceed 500 C., so far as I am aware (Lewes, Journal Society of Chemical Industry, vol, XI, page 585) and are not such high temperatures (700 to l000 C.) as are used for making oil gas by the known methods of Pintsch, Fritzsche or Ullmann.

The invention will therefore now be describedas carried out upon the gaseous efflux of vapor phase cracking of petroleum so contrived as to produce a vaporous and gaseous eiiiux which, when stripped of a motor spirit fraction, is exceedingly rich in the oleine substances above mentioned. But it will be understood that this process is applicable without change, except in degree, to the treatment of other complex oleine mixtures, and that the specific instances now to be described are described by way of illustration of the invention, and are not to be viewed as comprising every instance of practice according to the invention.

In the accompanying drawing, the ligure is a diagrammatic flow sheet showing a preferred assemblage of apparatus illustrative of certain physical stages of separation of the material treated.

The process to be described comprises, in' general, submittin the olefine-bearing gases to treatment for t e physical separation of fractions containing groups of olene substances capable of chemical segregation concomitantly with the formation of olefineacid compounds, emulsions, or solutions, un-

der conditions permitting the segregation severally of derivatives, for example alcohols A resulting from hydrolysis ofA these compounds.

Referring to the drawing, a container 1 for the suply of oil may deliver to a feed stock reservoir 2, whence by a suitable pressure device 3 the material is forced into a preheater or primary Vaporizer 1 (preferably a suitable tubular coil) and through a superheater or secondary vaporizer 6, which may be substantially the same kind of tubular heater as the primary preheater 4. Between the preheater 4 and superheater 6 the iiowing stream, already substantially all vapor, 16 may be subjected to treatment adapted to separate out the inclusions of lowvolatility, and pass on the vapors and gases. A liquid separator 5, preferably of a kind operating vwithout substantial loss of heat, is recommended. Collected liquids from this separator may flow through a pipe 6a and a cooler C to tar storage tanks 10. Y Vapors superheated at 6 pass to a cracking tube 7. The eliiuent gases, vapors and susl5 pensions from cracking are recommended to be treated in a separator 8, which may work on the Cyclonic or centrifugal principle, and

deliver its liquid separates into the pipe 6a,

and condensing towers, for example, the tower 11, adapted to counter-current flow in contact of the vapors and gases and the condensate from tower 12, which in turn is adapted to ,counter-current iiow of the vapors and gases and the condensate from a fractionating condenser 13 ofany suitable reflux t e.

Q yhe tower 12 is preferably a fractionating tower of the bubble type. From the bottom is taken a relatively heavy fraction which is delivered into the top of tower 11, wherein it serves to condense and wash out any heavy and undersirable tars formed in the cracking reaction. From one of the lower plates of this tower is drawn off a fraction of substantially the same boiling range as the feed 50 stock, but as this will, of necessity, contain .it cannot be returned to the feed stock without materially decreasing the yield of motor spirit. Provision is included, therefore, for stripping this fraction of its lighter hydroc'arbons, such as a fractionating tower 12a, which is heated at the base at 14 and delivers .overhead the desired fraction of its feed into one of the top plates of tower 12. The stripped cycle stock is delivered through a pipe 14a and cooler/G to the feed stock tankA The overhead from 13 is cooled at 18, and the condensate at this point is crude motor spirit in the preferred operationof and its vaporous and gaseous eiliux into the bottom o f the first of a series of separating some hydrocarbons in the motor spiritrange,

now fractonally condensed or absorbed, or otherwise treated to separate oleine fractions, which from their preponderant contents, may be described as an amylene fraction, a buty- The vaporous eliiuent from condenser 18 is lene fraction, and a gaseous fraction rich in propylene and ethylene, and hereinafter referred to as a propylene fraction'. For example, the gaseous eiiluent from condenser 18 may be delivered through meter `M and scrubbed in absorption towers 2O and 21 by a counter-current iiow of cool absorption oil stored in tank 23, delivered by a pumpi P1 through a cooler C2 and pipe 24 to the top of tower 21, to receiver 25, pumped at P2, through a cooler C3 to the to`p of tower 20, and the saturated oil delivered through a pipe 26 to a storage tank 27, whence the saturated oil may iow through a heat exchanger 28, pipestill 29 and vaporizer 30 to a refluxing tower 31, from which the liquids may be'led through cooler C4 to the crude motor-spirit or gasoline storage tank 16 by pipe 32. Unvaporize'd absorption oil from vaporizer 30 ,may flow through pipe 30a, heat exchanger 28, and cooler C5 to tank 23. I

'The vaporous eliuentat 33 may be delivered through a condenser 34 and a' separator 35, whence the vapors pass to a compressor 36 and pressure storage tank 37. Condensates at-34, and 37 may be delivered to tank 17, the pressure and temperatures being such as to provide at these points liquid fractions corresponding to the amylene-fraction liuid in tank 17. Pressure tank 37 may deliver, ifdesired, through a suitable reduction valve 39 to gas-holder 40, in which are 'collected the residual gases fromthe satu rated scrubbing oil. This gaseous fraction, if so separated, represents substantially the major portion of the butylene hydrocarbons,`

whereas the residual gas from tower 21, coll lected in the holder 22, contains the propylene and ethylene.

Whenappropriate conditions are realized in and prior to flow through the cracking tube 7, the respective fractions capable of being separated by steps of condensation or' absorption are sharply characterized by the desired preponderance (amounting under good conditions to substantial freedom from mixture with each other) of the oleine substances. sought to be collected and separated. vAny suitable condensation or absorption fractionating treatment may therefore be resorted to, and the apparatus mentioned may be varied in accordance with engineering preferences..

abovedescribed and the segregation of the olenes. into comparatively simple fractions shows the'y relative amounts involved and the quantity of each fraction:

. Results of .S2-hour run (quantities per bbl. through out) 5 1. Gas oil used, 31 Baum.

2. Crude motor-spirit recovered r14.5 lbs. 3. Cycle stock 110 lbs. 4. Fuel oil. 30 lbs. 5. Process gas at M (rich gas)- 80 lbs. (1040 cu. ft.) 6. Residual gas from compressionto 250 pounds per sq. L 33.4 lbs. (533 cu. ft.) 7. Pressure condensate'. 40.61 lbs.

Products from pressure condensate 8. Amylene fraction (liquid).

(ag Up to C 4.51lbs.,

(b 25.-45C 5.151bs. 9. Butylene fraction (gaseous) 19.6 lbs.(181 cu. ft.) 10. Light naphtha (included in 2) 11.35 lbs.

These'results are from separation by compression, distillation and condensation. When the absorption step, as described above, is resorted to, typical results are as follows:

20 reed stock-sanar Be. gas ou (from south Texas crude.)

Feed rate-l bbl. per hour per six inch cracking tube. Temperatures- Va orizer 632 C. maximum Tu e 601 C.' (average) y' Tube sections (averages) ,25 Entrance 2 3 4 5 6 595 C. 602 C. 602 C. 603 C. 606 C. 603 C.

Conversions per bbl. passed i1 scrubbed gas (up. gr. 0.929) 1035 cu. ft. Process gas (s gr. 1.05 675 cu. ft. Butylene fract on (non-condensed gas from distillation of saturated ab- 102 cu. ft.

sorption oils) (sp. gr.--1.52)

Amylene fraction (condensibles recovered by fractionation to 60 C. 2.6 gallons Crude naphtha (condensibles between 60 and 210 C.) 9.3 gallons Cycle stock (condensibles above 210 C.) 19 gallons Tar residues 2.1 gallons Olefine content of gaseousl fractions:

Process gas olenes above ethylene.. 33.1 Oil scrubbed gas oletines above ethylene 17.8

or oil scrubbing to remove condensibles may be as high as 54% by volume in the operation of an appropriate vapor phase craclng process, `for-example that described. For comparison, the oleine content of pressure-still gases is seldom higher than 10%, and is usually under 8%, justifying designation as lean gases.

The aggregate chemical character of these two classes of oleine mixtures is likewise quite different, so that steps for the recovery of derivatives applicable to the lean gases are not applicable to the richer mixtures. The olefines in pressure-still gases have a high proportion of normal oleneS, and do not contain substantial amounts of the very reactive, hi Vhly cracked hydrocarbons, such as thef=diole nes.

The recommended steps above described, for which other procedures may of course be substituted within the invention so long as the results are produced, result in a fractionation of the olefines as follows: i

n. Bolling points:

Ethylene -103 C.v

Gaseous Propylene 48.4C.

Iso-butylene C. Butylenes Butene1 C. Butcne2 i C.

' Boiling points: Isopropyl ethylene 21 C. y Uri-syl'lmi methyl-ethyl- 31 t C* et yene o3' Li` id Anl-vienes Pentene-2 36 C. l qu v Trimethyl ethylene 37 to 42 C. Pentenel 39 to 450 C.

V Hexylenes 55 to 75 C.

Higher olefnes, upy to 150 C.

Associated with the amylenes and butylenes are substantial inclusions of diolefines, believed to be butadiene, isoprene, and their homologues.

7e are aware of no practical arrangement of conditions or procession of reagent substances by which any Whole mixture of these gaseous substances can be treated to yield in succession the derivatives of the unsaturated hydrocarbons present in them in amounts constituting valuable sourc`es of' materials needed for industrial uses. Butwe have nevertheless determined that the substances are reactive with the polybasic acids, for example sulphuric acid, in a 'certain order, ethylene .being the least reactive as follows:

Boiling points 1 State 1. lilthylenevCH2=PFrn -103. C. Gas 2. Propylene CH3-CH=CH J 48.4 C. Gas 3. Pentene-il CH5-CH2-CH2-CH=CH 39-4 Liquid 4. Pentene-2 CHS-CHg-C =CHCH 36 C. (741 mm.) Liquid 5. Butenel CHa-CH-CH=CH2 5 C. Gas tait in s0- u on 6. Butene-2 CHq-CH=CHCH3 1 C. Gas or in s0- 7. Isopropyl ethylene ICH; lution CHCH=CH1 21.1 C. Liquid o CH 8. Unsymmetrcal methyl ethyl CH ethylene C=CH1 31 to 33 C. Liquid CHXI-CH 9. Tl tb l eth lene- CH CH r me y y 37 to 42 c. Liquid CH H t l CH 10 liso-bu y en? C=CH, 6 C. Gas or in so- CH lation To absorb ethylene and produce ethyl sulphuric acid it is necessary touse hot concentrated acid which will substantially polymerize all other oleines above propylene in reactivity; the propylene will also be 'polymerized.

With 100% acid below 30 C., there is no appreciable. absorption of ethylene and the absorption of propylene is very rapid, but the yield of isopropyl alcohol will be small due to the excessive polymerization when and if the gas treated contains the more reactive olefines in the amounts in which they naturally occur.

The following. causes may be responsible for this phenomenon:

(l) The reactive olenes evolve so much heat on contact with-the sulphuric acid that local overheating occurs which tends to polymerize all the dissolved products including propylene.

ethylene and of the proper strength and under the optimum conditions to'labsorb the `oletines which yield tertiary derivatives (Nos. 8, 9, 10 above) there is no substantial absorption of the lighter and simpler oleri-nes such as propylene. For a quantitative videa of the great variations in reactivity manifested by these olefines towards sulphuric acid, isobutyleneis several hundred thousand times as reactive as ethylene.

In the case of isopropyl ethylene, which so far as we are aware has never, previous to the research leading to this invention, been converted into an alcohol through reaction with sulphuric acid, acids of suiiicient strength to absorb 'pentene-I and pentene-2 quantitatively polymerize isopro yl ethylene at temperatures below 30 C. igher temperatures and more concentrated ac id than this are required to absorb the other oleines for the results desired, and the conditions' for securing a good yield of'amyl alcohol from this particular olefine substantially polymerize the other olefines except ethylene and propylene present inthis mixed gas.

By the fractionating procedure above described we have-avoided any necessity to subjectl to sulphuricacid absorption all of the reactive olefines at once, and any necessity for, producing alcohols -incapable of being subsequently separated.-

By processes" extending and developing the results of this invention, some of which are the work oi others and 'no part of this inven- I tion, at least eight dierent alcohols may be produced from the vapor-phase cracked hydrocarbons, having a boiling range extending from 80 to 140 C.

If these were produced conjointly it would be impractical subsequently to separate them,

and as the uses (of isopropyl and amyl alcohols, for example) are widely divergent, such a mixture would be of little or no commercial value. As a specific example of this difficulty two pairs of alcohols that`cannot be separated b v fractional distillation are:

Isopropyl alcohol (constant boiling mix-'- ture)-boiling point 80.4-C.

Tertiary butyl alcohol-boiling point 79.92" C.

1o1.6 to 102 o. a Sectidary butyl alcohol-boiling point Tertiary amyl alcoholboiling range The processing of the total olenes preslent .in a cracked petroleum product to secure tertiary as well as secondary derivatives calls for a further departure from the art as practiced where tertiary derivatives are not recovered. The usual procedure is to moderately dilute the product from sulphuric acid absorption with Water and then distill. The point to which this dilution must be carriedto avoid destruction bythe action of the sulphuric acid on the alcohols during distillation varies with the different alcohols but in the case of secondary alcohols there is little hazard in distilling from 25% acid solution.

Tertiary alcohols, however, behave quite difcentages of tertiary bodies as compared to secondary bodies. It becomes practical and feasible when the tertiary bodies are concentrated and segregated as in the practice of this invention.

The procedure above described, to avoid the difficulties and provide the advantages just adverted to, separates the material into groups capable of being reacted upon preferentially in respect to their constituent members, thus enabling separations of the acid combinations with the constituent members of these groups severally. So far as there is advantage in separating them, these groups are:

(1) The gaseous fraction containing ethylene and prophylene.

(2) The butylene fraction containing isobutene and butene-l or butene-2 or both of the initial low-boiling distillate fraction, and

(3) 'Ihe residue of the condensate which may contain each of the five isomeric amylenes, with varying amounts of hexylenes and higher olefines.

' Fraction(1)may now be treated iu accordance with the specific relative properties of. its constitutents.

Because this fraction will contain traces of diolefines and olefines more reactive than propylene, owing to the practical and obvious limitation .of any system for physical fractionation, it is desirable to treat this fraction first with sulphuric acid, by tower scrubbing, of astrength that will selectively react upon the olelines (more reactive than propylene) therein present. In

the preferred procedure this fraction is first scrubbed with acid of 80-84% strength and is then subjected to the action of sulphurlc acid having a concentration from 95 to 100gb at a temperature preferably below whereupon propylene is substantially absorbed. The ethylene remains relatively unaffected and may be preserved and usedy in the gaseous condition, or subsequently be reacted upon, as for example by absorption in hot sulphuric acid resulting in the formation of ethyl sulphuric acid; or treated in any known way to produce ether. Specific and preferred modes of treating fraction (l) for the recovery of these values form no part of the present invention.

Gaseous products belonging to other series of hydrocarbons which may be present in minor quantities as impurities, either remain in'the gaseous state, as in the case of methane or ethane, or remain unabsorbed by the acid treatments; or, as in the case of acetylenes, are converted into heavy compounds readily separable from the remainder, as by fractional distillation. If present, such bodies are not found in important quantities, and the resulting polymer vis a heavy oily compound, ofrelatively uniform characteristics. InV practice with hydrocarbon mixtures 'obtained as herein described the proportional respectively may be recovered in the distil/ lates, leaving a residue of substantially alcohol-free sulphuric acid.

The butylene fraction (2) capable aof economic use contains b utylenes dificult to separate from each other by distillation. Of these butene-l and butene-2 are less reactive chemically than iso-butylene. Derivatives of butene-l and butene-2 as a consequence of ,the intramolecular structure of these substances have a secondary molecular formation, whereas derivatives of iso-butylene have a tertiary structure. This may How from the structure of isovbutylene, conceived as a central carbon atom linked to threeother carbon atoms, one inter-carbon bond being a double bond. As for example, the addition of water (H2O) produces a tertiary alcohol having the structure: v

. om on v 0113 C CH3 Preferred procedures therefore comprise reacting upon-the butylene fraction in the order of reactivity of these component substances, to form in several succession tertiary and secondary derivatives.

For example, the butylene fraction containing isobutene, butene-l and butene-Q (all gaseous) is passed through sulphuric acid of a concentration of more or less in such manner as to effect as intimate a contact between the gas and the acid as possible, for the purpose of absorbing isobutene; Recommended apparatus comprises an interrupted flow tower with glass or other inert packing arranged for counter-current fiow of gas and acid. Isobutene is very highly reactive; a satisfactory differential absorption is practicable at all ordinary temperatures. The isobutene is here selectively absorbed, leaving the butene-l and butene-2 and other gases, if any, which are then conducted through sulphuric acid of a concentration of 80%, more or less` by^which the butene-l and butene-2 are substantially absorbed. One of the advantages ofthis procedure arises from having removed the substances reacting to tertiary compounds, since the reaction of the secondary-alcohol-forming substances with stronger acid for their conversion evolves heat of lesser degree, and the natural rise of temperature, for example to 40 C., may be permitted to take place, unless acid more concentrated than 80% is resorted to, in which case it may be desirable to hold the temperature down to a point below 15 C. These reactions are preferably carried out in a tower similar to the tower just mentioned; one tower may be used if arrangement is made to collect the gaseous eillux and repass it, supplying the more concentrated acid on the sec-` ond passage and separately collecting the liquid `eti'lux from the first and the second passage.

The liquid from the first of said steps contains the isobutene either absorbed in the acid or in the form of tertiary butyl alcohol by auto-hydrolysis in the ,dilute acid; this may be further diluted for complete hydrolysis and the alcohol -distilled therefrom. Preferably the dilute liquidis neutralized with an alkali before distillation, to result in a much higher yield of the tertiary butyl alcohol by avoidance of reaction with the acid during distillation. A

The liquid fromthe second step of treat- -ment contains the butene-l and butene-2and thereafter distilled without neutralization tov obtain a high yyield of secondary butyl alcohol. The distillate may be dehydrated, if desired, by any usual or customary waterabsorbent chemical treatment, such as treatment with lime or caustic. Y

The amylene fraction (3) Whether collected by absorption as described or by pressure condensation and fractional distillation of fraction (l) (propylene, ethylene, etc.) consists preponderantly of the amylenes and may contain hexylenes and higher olefines as Well as hydrocarbons of the group CBHZH. This liquid mixture, which typically contains less than 5% of paratiins, may advantageously be distilled into three parts corresponding to temperatures (a) Up to 25 C. (b) 25 t0 45 C. l (c) Above C.

Since the lower or more volatile olefines have been substantially removed as above described, distillate (a) consists primarily' of isopropyl ethylene, distillate (b) of pentene-l, pentene-2,A unsymmetrical methylethyl-ethylene, and trimethyl ethylene, and distillate (c) contains the hexylenes and heavier or higher boiling olefines.

The amylene fraction (3) can be treated with sulphuric acid in stages, or the fractions (a) and (b) can be'processed separately and with some advantage.

Distillate a) contains predominant quantities of isopropyl ethylene. rPhe specific treatment of this distillate forms no our 'invention herein claimed.

In order to secure substantial 'yields of all alcohols derivative from the mixed `amylenes offraction (b) it is desirable to remove the hydrocarbons of the group Chl-LM (and any still less saturated hydrocarbons) which may be present. Either of the alternative processes is satisfactory at this stage.

It has been found, for example, that b v treating this fraction first with concentrated hydrochloric acid, the amylenes which are convertible into tertiary derivatives are lsub` stantially converted into chlorides which,

owing to their relatively high boiling points,

' can be easily separated from the unchanged fam'ylenes. The resulting mixture of chlorides on hydrolysis, carried on preferably with the addition of lime or caustic soda,

iyields tertiary alcohols.

We do not herein claim the specific method of recovery with the aid of hydrochloric acid treatment.

part of `tertiary alcohols.

more or less, which promotes the formation of tertiary alcohols by bringing about the addition of water to. isobutene trimethyl, ethylene, unsy'mmetrical methyl-ethyl-ethylene and probably some of the higher olefines while concurrently effecting the polymerization o'f diolefines and those hydrocarbons of a lesser degree of saturation than the olefines into heavy, oil-like polymers which, on account of diversity of boiling points, may be separated by fractional distillation, or. other izppropriate means, from 'the unchanged olenes.

As the result of this preliminary reaction, fory exampleeither the said hydrochloric or sulphuric acid treatments, a highly refined amylene fraction remains after treatment, which fraction is substantially a mixture of isopropyl ethylene, pentene-l and pentene-2, Vand which does not contain appreciable amounts of the other olefines, though there is mation of the corresponding-intermediates' of the alcohols from which'the correspond- .ing alcohols may be recovered by dilution and distillation.

To further illustrate the advantage of this invention we have treated the rich gas from vapor phase cracking as described, without first removing the amylene fraction, with 95% acid. The result was an evolution of eX- cessive heat, rendering control difficult, if not impossible, amounts only of secondary alcohols, and no There were als formed large quantities of heavy tar-like polymers. By first -removingthe olefines higher than' and' the recovery of small propylene we have successfully used fuming For specific examples of treatment of the` amylene fraction 3,(6) we have obtained the following results:

Example 1 From theprocessing of 32 B. gas oil under the conditions mentioned forexample above,'there is obtained 2.6 gallons of amylene fraction (condensibles recovered by fractionation to 60 C.) per barrel passed. The preferredtreatment of this fraction and its results are as follows:

To the .2.6 gallons of amylene fraction wel first add 12.2 lbs. of sulphuric. acid (65%) hours as a maximum, adding the acid in two equal portions lat 3 hour intervals. At the end of this period agitation is stopped and the mixture allowed to settle for a time suiiicient to result in separation into two welldefined layers. We first draw off the lower or acid layer, which is carefully neutralized with caustic and distilled, preferably through a fractionating column, cutting when the temperature reaches 100 C. at the top of the column. Under these specific conditions we recovered in this example .28 gallons of crude tertiary alcohols per 2.6 gallons of amylene fraction treated.

The residual hydrocarbons from this treatment to recover tertiary alcohols are distilled through a fractionating column from a slightly alkaline mixture, and the distillate up to 60 C. is segregated and treated for conversion into secondary alcohols.

Starting with 2.6.gal1ons of amylene fraction, there is recovered 1.1 gallons of hydrocarbons boiling up to 60 C. which are now treated with 77% HQSO4 in two portions,

p each of .55 gallons or 7.65 lbs. In this stage the temperature is allowed to rise to 35 C( and maintained at under 40 C. preferably, and agitation is continued over a total period of six hours. The mixture is then allowed to settle and the lower or acid layer is drawn off, diluted with water to bring the concentration of ac'id belowv 20%, and then distilled` until practically all of the alcohol is carried over. The distillate consists of two layers, a lower or water layer and an upper or alc ohol layer. From thev 2.6 gallons of amylene fraction at the start of this processing, there is recovered under the above specific conditions .56 gallons of crude secondary alcohols.

Secondary and tertiary butyl alcohols are successfully recovered from the butylene fraction by first scrubbing with 65% more or less sulphuric acid, and then with 77% more or less sulphuric acid, as above described.

'Exam-ple? Concurrently with the production of 2.6 gallons of amylene fraction there is recovered 102 cu. ft. of butylene fraction as set forth in the example above of a typical vapor phase cracking operation. As stated, this fraction can be absorbed under pressure or by cooling or both in the amylene fraction; or ity can be treated separately to produce tertiary and secondary butyl alcohols. The following is an example of separate treatment;-

The butylene fraction is first scrubbed or treated with a relatively dilute sulphuric acid, followed by more concentrated acid.

We have obtained satisfactory results by using in the first absorption stage 65% acid and in the second 77% acid. The amount of acid required depends upon the physical efliciency of the absorption apparatus employed in large measure; using even comparatively inefficient apparatus, an acid efficiency can be realized wherein three pounds of acid (calculated as 93%) produces one pound of alcohol. From the treatment of 100 cu. ft. of the butylene fraction herein described, we have produced .28 gallon of tertiary and .46 gallon of secondary alcohols. l

During the absorption of the butylene in the treatment for tertiary alcoholwith the particular reagents mentioned above we prefer to keep the temperature below 20 C., and during the secondary Istage at about 35 C. As in the case of the tertiary am l alcohol, it is tnecessary to distill the tertiary butyl alcohol from a neutral or slightly alkalinek solution to secure the highest yields, though tertiary butyl is not subject to decomposition in acid distillation in the same degree as tertiary amyl alcohol.

Whereyer in this speclication particular concentrations of acid reagent substances adapted to olefine absorption are alluded to, it will be understood according to the common knowledge of the numerous chemists familiar with the behavior of acids toward olefines for nearly a century, that ythe acid concentration is lrelative to the respectively mentioned or to normal temperatures, and that at different temperatures another concentration of acid is equivalent, within thoseV limits at which the action of the acid reagent ceases to become an absorption, and enters upon the destructive formation of the compounds herein alluded to as polymers.

For the operations of fractional treatment with H2804 e. g. of the amylene fraction (b) we recommend the use of apparatus comprising a chamber adapted to be heated or cooled, and equipped for mechanical agitation of its contents; adapted for the slow feed of acid of the appropriate concentration; suitable settling vessels for decanting olf the unchanged residue of the materials of lesser reactivity; and appropriate vessels for acid reaction upon the decanted residue. Distillation of the oletine-acid liquors may proceed in appropriate steam stills. In essentials, the units of apparatus required are familiar in the practice of the chemical industries, "and one of the' advantages 4of this invention resides in the relatively simple nature of the l accomplished by contactin fraction b admixin atoms-to the molecule, the

'tion and a temperature .predominantly o Ybon atoms to the molecule c stantially free from olefines of 4 and more carbon atoms to the molecule, the said fraction containing olelines of 2 and 3 carbon atoms to the molecule, and selectivelyr sulphatin olefines of 3 carbon atoms to the. molecu e contained in said fraction by1 ad'l mixing said fraction with aqueous sulp uric acid, while maintaining an acid concentraat which sulphation of the said olefines of 3 carbon atoms to the molecule takes place with the resultant formation of propyl sulphate.

2. Process according to claim 1, in which the selective sulphation of olenes of 3 carbon atoms to the molecule in said fraction is said fraction with aqueous sulphuric aci of from 95 to H2SO4 content. e

3. Process according to claim 1, yin whichthe selective sulphation' of olelines of 3 carbon atoms to the. molecule .contained in said fraction is accomplished by contact g sai fraction with acgleous sulphuric acid o from' 95 to 100%, H2 O4 content, at temperatures not exceeding 30 C. f

4. In the process of generating isopropyl alcohol from a mixture of hydrocarbons produced by crackin petroleum oil consisting olenes and containing olenes of2, 3, 4 and 5 carbon atoms to the molecule, the steps of separating from said mixture by distillation a fraction, substantially f ree from oleines of 4 and more carbon atoms to the molecule and containin oleines' of 2 and 3 carbon atoms tothe vmo ecule, andselectively sulphating olelines of 3 carbo'n atoms to the molecule said fraction with aqueous phuric aci while maintaining an acid concentration and a' tem rature'A at which sulphation of thesaid o efines of 3 carbon atoms to the molecule takes place with contained in said carbon atoms tively sulphating oleiines of 3,v

ecule contained in said fractionby to the mo admixing said fraction with aqueous sul'v phuric acid, 'while maintaining an acid concentration and a temperature at which sul-v phation of the said olenes of 3 carbon atoms to the molecule takes place with the resultant formation of propyl sulphate'.

8. Process according to the selective sulphation of oleines of 3 carbon atoms to the molecule contained in said said from fraction vis accomplished by contactin fraction with a ueous sulphuric acid o 95 to 100%, H2 O, content.

9. Process according to claim 7 in which the selective sulphation of olenes of 3 carbon atoms to the molecule contained in said fraction is accomplished by contacting said fraction with atgleous sulphuric acid o from 95 to 100%, H, O, content, at temperatures not 'exceeding 30 C.

, wanmcn J. MURRAY.

claim 7, in ywhat l 'lal the resultant formation of ropyl sulphate.

5, Process accordingto c aim 4, the' selective sulphation of olefines of 3 carbon atoms to the molecule contained in said Ain which 6. Process according to claim 4, in which the selective sulphation of o eines of 3'cartained in said fraction is accomplished by contactin said fraction with aqieous sulphuric acid o from. to 100%,]1, 04 content, .at temperatures not exceeding 30 C.

7. In the process 'of generating isopropyl alcohol from a mixture of hydrocarbons pro duced by.` vapor phase cracking of petroleum1 'oil' consisting predominantly of olenes and containing olenes of 2, 3, 4 and 5 carbon ing rom said mixture by distillation a frac-v tion, substantially free from olefines of 4 and 

